Treating hydrocarbon fluids



m..4 6. 4 9 l 3 ,2. P A

3 Sheets-Sheet l Filed Deo. 50, 1.941

Nowu h n mi .ESS mi@ WK wm @v LUSS mi. Y WRRRW IV. .wh 1

NlNhN April 23, 1946. y H. z. MARTIN y 2,399,

TREATNG HYDROCARBON FLUIDS Filed Deo. 30, 1941-, 3 Sheets-S1196# 2 QEcE/VEEA Tgp@ divides form is heat t the liquid feed lis oi the .upilow type,

'2.399.050 Y mesmo mnocAnsoN noms Romer Z. Martin, Standard 0l] ration of Delaware 'rms inventionrelates to catalytic tions involving the production of hydrocarbons of relatively low boiling point suitable ior'use as motor fuels. According to this invention catalyst in nnely mixed with solidinert particles in nely divided form so that a mixture oi solid particles is obtained which when regenerated after a catalytic reaction will supply sumcient to vaporize it and maintain it at reaction temperature in a reaction zone.

For example, in the catalytic cracking of hy drocarbons, carbonaceous material is depositedcnthe solid particles during cracking and when the solid particles are regenerated as by burning to remove the carbonaceous material, the solid particles are heated to a temperature above the cracking temperature and when these heated solid particles are mixed with the oil feed the oil feed is vaporized 'and heated to a cracking temperature. superheating furnace such as a coil heater for vaporizing the oil feed is. eliminated. Also regeneration coolers lfor controlling the temperature in the regeneration zone during regeneration are eliminated and the hot regenerated solid particles are used without any intermediate cooling for mixture with the oil feed. l

Several forms oi the -invention are shown in the drawings and will be more speciiically described in the description hereinafter. y

In the drawings:

Figure 1 represents one form of apparatus adapted for carrying out the invention in which the regenerator is above the reactor and solid particles are withdrawn in a dense phase from the bottom portion of both the regenerator and the reactor;

Figure 2 represents another form of apparatus Cranford, N. J, Development Com vassigner te Dwynmvof museum December so. 1an, senaat. 42ans vs cum.. wi. zt-zss) and more particularly relates. to' catalytic reac are withdrawn from the regenerato'rV l2 by means having a suitable control valve )it for' controlling the amount oi solid particles Using thisinvention, a heating or.

adapted forl carrying out the invention in which the regenerator is supported near the ground and whereas the catalyst in a dense phase is removed from the bottomportion of the reactor; and 4 Figure 3 represents another form of apparatus adapted for carrying out the invention in which the regenerator is in an elevated position and of the bottom draw-oil' type whereas the reactor is at a lower level and of the upflow type.

Referring now to the drawings and to Figure 1. the reference character lll designates a reaction zone or vessel and the reference character I2 designates a regeneration zone or vessel. Solid `particles including inert and catalytic 'particles directly introduced into the reaction zone ld. The solid particles undergoing regeneration in the regeneration zone l2 are maintained in a fluidized condition and flow therefrom through the standpipe Id like a liquid. As will be later pointed out in greater detail, the solid inert particles act as heat carriers and are used ,because catalyst'only in such large amounts would render the reaction uncontrollable in certain reactions as in catalytic cracking of hydrocarbon oils.

Liquid oil feed, preferably preheated, is introduced into the bottom portion oi the reactor l0 through line I8. The solid particles including the inert and catalyst particles are maintained in a'iiuidized condition in the reaction zone id and in this way the solid particles are maintained in a turbulent condition and the temperature in the reaction zone is' substantially uniform. The level of the iluidized mass in the reaction zone I0 is shown at 22. The level 22 is not quiescent but is more like the surface of a violently boiling liquid. The lower end of standpipe lll extends below the level 22 of the iluidized mass in reaction zone It.

As shown in the drawings, the reaction zone is avrelatively shallow cup-shaped receptacle or vessel which is concentric with and arranged in the lower part of a. larger vessel 2d. The reaction vessel I0 is suitably the larger vessel 24 by means diagrammatically shown at 28. As the reaction lzone i0 is oi a smaller diameter than the larger vessel 2d, an annular space 28 is provided tion zone l0 andthe larger vessel 24 into. which the solid particles overflow from the reaction zone I0. Suitable stripping gas is introduced into the solid particles in the annular space 28 by means of line 32 to remove volatile hydrocarbons from the solid particles.

'I'he velocity of the vapors passing through the solid particles in the reaction zone I 0 is selected to maintain a fluidized mass therein. As more oil and more solid particles are fed into the' reaction zone I0, the reaction products in vapor form pass upwardly into the enlarged space 36 in the enlarged vessel 24 and this enlarged space forms a settling chamber for removing solid particles from the reaction products. In addition, the iluidized solid particles in relatively dense con'- dition overiiow the upper rim of the reaction vessel I 0 and ow into the annular space 2t where additional quantities supported on the bottom of between the reac` of vaporous reaction prod-4 nular space are also maintained in fluidized condition but their density is greater than the density of the-fiuidized mixture in the reaction zone` The reaction products in vapor form pass upwardly from the enlarged chamber 34 and preferably pass through additional separating means shown diagrammatically at 36. If desired, cyclone separators may be used. If the upper narrowed portion 31 of the larger vessel 2l is enlarged to form a settling chamber, the additional separating means shown at 36 may be eliminated. The upper narrow portion 31 is closed at its upper end by a partition plate 81'.

The vaporous reaction products leave the upper portion of the vessel 24 through line 38 and are introduced into the lower portion of a fractionating tower 40. The reaction products contain a small amount of solid particles and these solid particles are removed in the lower portion of the fractionating tower as will be hereinafter described in greater detail.

In catalytic reactions where the solid particles become contaminated or partially spent after a reaction period it is necessary to regenerate the solid particles. For example, in the catalytic cracking of hydrocarbons, carbonaceous material is deposited on the catalytic and solid particles and the catalytic and solid particles are regenerated by burning off the carbonaceous material. The used solid particles containing catalyst are withdrawn from the annular space 28 by means of-standpipes 42 provided with control valvesM. The standpipes l2 communicate with the bottom portion of the draw-on compartment 28 and the solid particles flow from the draw-off compartment 28 into the standpipes 42. A suitable regenerating gas such as air or other oxygen-containing gas is introduced through line 46 into branch lines 48 and 82 for introducing the regenerating gas into the used catalyst and solid particles withdrawn from the annular chamber 28.

As above stated, the fiuidized solid particles act like a liquid and produce a pressure atr the bottom of the standpipe 82 which is suflioient to carry the solid particles to the regeneration zone I2.

By introducing a regenerating gas below the valves M, a light suspension of solid particles in a gas is formed and the pressure produced by the column of dense solid particles is suiiicient to force the used solid particles upwardly in the branch lines 5I and 56 for returning the solid particles to the regeneration zone I2. In addition to this column in Figure l, there is a pressure of about 8 pounds per square inch gauge in vessel 24 and reaction zone III and this pressure is added to the column to return the solid particles to regeneration zone I2. The regeneration is under 1a pressure of only about 1 pound per square inch gauge. The used solid particles are introduced into the regeneration zone below a perforated distribution plate 58.

The. velocity of the gas mixed with the solid particles being regenerated is so selected that the solid particles are maintained in arelatively dense fuidized condition and have a level designated at 62. The level 62 is not quiescent but resembles a violently boiling liquid. While the level 62 is shown at one position in Figure l, it is/understood that this level may be varied and may be at higher or lower levels for different reactions or for different oil stocks. Above the level 62 the regeneration zone I2 is provided with an enlarged chamber B4 which forms a settling chamber for separating solid particles from the gases of re generation. The gases of regeneration pass overhead irom the enlarged chamber 64 through line 66 and are further treated to recover residual amounts of solid particles and for preheating the liquid feed when it is a low coke-forming stock as will be presently described. When the liquid feed is of a high coke-forming stock it is preferably cooled after passing through the scrubber presently to be described.

The standpipe I4 used for conveying hot regenerated solid particles from the regeneration zone I2 to the reaction zone III has its upper end 68 extending above the distribution plate 58. In

this way the solid particles are withdrawn from the body of the fiuidized mixture in the regeneration zone I2. The regenerated solid particles in standpipe Il may be stripped of oxygen-containing gas by introducing a stripping gas such as steam through line B9.

The gases of regeneration passing through line 66 are passed through a suitable cooler B9 provided with vertical tubes 12. A heat exchange medium is circulated through the heat exchanger and around the tubes 12 through inlet line 14 and outlet line 16. The cooled gases of regeneration are then passed through line 18 and introduced into the bottom portion of a scrubber or scrubbing tower 82.

Liquid feed such as liquid oil is passed through line 84 by means of pump 86 and is introduced into the upper portion of the scrubbing tower 82. The liquid feed is sprayed into the upper portion of the scrubbing tower 82 by means of a spray device 88. The falling droplets of liquid feed scrub out any entrained solid particles and at the same time the liquid feed is preheated by absorbing heat from the hot gases of regeneration. The scrubbing tower may be provided with baffles, discs and doughnuts or packing to provide a large surface for contacting the oil with the gases. The cooled and scrubbed gases of regeneration leave the top of the scrubbing tower through a valved line 82 and may be vented to the atmosphere.

The preheated liquid feed when it is of a low coke-forming type and containing the solid par-i ticles scrubbed out of the gases of regeneration is withdrawn from the bottom of the scrubbing tower 82 through line 94 and is passed to coil 98 in heat exchanger 91 by a pump 98.' In the heat exchanger 91 the oil feed or liquid feed is indirectly contacted with bottoms containing solid particles scrubbed from the vaporous reaction products and withdrawn from the fractionating tower 40 through line H12 by means of pump |84 and passed through line |06 and through the heat exchanger 81. The partly cooled bottoms are withdrawn from the heat exchanger through line |08. The preheated liquid feed leaves the heat exchanger 91 through line II2 and may be combined with at least a portion of the cooled bottoms passing through line IM and the mixture passed through line. III;` and valved by-pass line I I8 and I I8' around heat exchanger or cooler H9 to the liquid inlet line I8 hereinbefore described.

When the feed is of a high coke-forming type the preheated liquid feed in line 94 is passed through valved line II'J' to line |20, by-passing heat exchanger 91. Valve |20 ahead of exchanger 91 is then closed. The high coke-forming stock is preferably passed through line |20 and yheat exchanger or cooler IIS to cool the feed oil. In some cases where the preheated feed stock is at the desired temperature, both exchangers 91 and I I9 may be by-passed and the feed stock passed through lines IIS' and H8' 'oil feed is to be passed through line |25, the valve in the by-pass line I Is isclosed.

The vaporous reaction products introduced into the bottom portion of the fractionating tower 40 are at a relatively high temperature and in order to desuperheat them and condense higher boiling constituents and also to remove entrained solid particles, at least a. portion of the bottoms is taken oi and cooled and returned to the fractionating tower 40. At least a part of the hottoms withdrawn through line |02 is passed through line |32 and heat exchanger |34 wherein the bottoms are indirectly contacted with a heat exchange` mediumintroduced through line |36 and leaving the heat exchanger |34 through line |38. Water may be used as the heat exchange medium and the steam produced may be used in other parts of the process.

The cooled bottoms are withdrawn from the heat exchanger |34 through line |42 and are passed through line 44 having a valve |46 which introduces the cooled bottoms into the bottom portion of the iractionating` tower 40. The line |44 at its outlet end in the Iractionating tower is provided with spray means |48 for spraying the cooled bottoms above a baiiie means |52 whereby intimate contact is provided between the vaporous reaction products and the cooled bottoms and entrained solid particles are scrubbed out to form a slurry. A portion oi' the cooled bottoms from line |08-may be introduced into line |44 and returned to the bottom of 'the fractionatlng tower 40.

The portion of the cooled bottoms -passing through line ||4 comprises a slurry and contains catalyst and solid particles which were washed out of the vaporous reaction products and the slurry formed is returned to the reaction zone I with the oil fed through line I8.

The vaporous reaction products pass upwardly in the fractionating tower where they are fractionated by contact with downflowing condensate oil and the desired product is taken overhead in vapor form through line I 54. Where relatively heavy hydrocarbons are cracked to form lower boiling hydrocarbons, the fraction or product taken through line |54 comprises gases and gasoline constituents which may be further treated in any suitable or conventional manner to separate motor fuel. In the treatment of hydrocarbons any desired side streams or fractions may ne removed from the side of the fractionating tower.

Referring now to Figure 2 of the drawings, the reference character |12 designates the liquid feed line to the reaction'zone |14. In this form of the invention the liquid feed preheating means and the fractionating tower for the reaction products have been omitted from the drawing. However, it is to be understood that the arrangement of coolers and heat exchangers and the A heat exchange medium is introduced scrubbing tower shown in Figure 1 are preferably used with the form of the invention shown in Figure 2. fr

The reaction zone |14 is similar to the reaction zone I0 described in Figure 1 and comprises a relatively shallow cup-shaped vessel which is supported in a larger vessel |15 by' means of suitable supporting means diagrammatically shown at |16.

Solid particles including catalyst particles are directly introduced from hopper |82 into the reaction zone |14 by means of standpipe |84 having a control valve |88. The solid particles are maintained in fiuidized condition in the reaction zone |14 and overow into the annular space |88 as described in connection with Figure 1 of the fdrawings. Stripping gas such as steam is preferably introduced into the denser fluidized mixture in the annular chamber |88 through line |92.

The spent catalyst or solid particles iiow into the standpipe |84 provided below the larger outer vessel |15. The standpipe |94 isprovided with as diagrammatically shown, at 2|2 may be used.

a control valve |98 near its lower end.

The i'iudized mixture in the reaction zone |14 has a level |91 and the iluidized mixture in the overiiow chamber |88 has a level |98. The height of fiuidized mixture from the level |98 to the valve |96 produces a pressure similar to hydrostatic pressure which is sufcient to force the spentl catalyst to the regeneration zone presently to be described.

Regenerating' gas such as air or oxygen-containing gas is introduced into the spent catalyst" and solid particles below the valve |96 by means of line |99 to form a relatively light suspension of solid particles in gas.l The light suspension is passed through line 202 and into the bottom of a regeneration zone 284. The velocity of the regenerating gas is so selected that a level 205 of fluidized catalyst or solid particles undergoing regeneration is formed in the regeneration zone 204. While the level 205 is shown in one position in Figure 2, it is to be understood that it may be varied and may be higher or lower with different oil stocks or different reactions. In this form of the invention it lwill be seen that the regeneration zone 204 is supported near ground level and in order to move the particles to a position above the reaction zone |14 an upilow regeneration zone is used. That is, all of the regeneration gases and the solid particles pass overhead from the regeneration zone 204 through line 206 and are passed into a separating zone 208 above the hopper |82 which feeds the hot regenerated catalyst to the standpipe |84 previously described.

The enlarged space 208 provides a settling chamber for separating regenerated solid particles from gases of regeneration. If desired, additionalcyclone or like separating means such The separated solid particles are collected in the hopper |82 with a level shown at 2|4. The gases of regeneration pass overhead through line 2|6 Y and in the preferred form of the invention a 1 for removing entrained solid cooler and scrubber are used as shown in Figure particles from the regeneration gases and also to recover heat from the regeneration gases Where a low coke-forming feed stock is used. If desired, a suitable fstripping gas such as steam may be introduced into the regenerated lcatalyst or solid particles in hopper |82 through ne 2|8. l

4 :,ssaosc 4 In the reaction zone |12 4the velocity oi the vapors passing therethrough is selected so that a riuidized mass ci solid `particles is obtained. The vaporous reaction products leaving the reaction zone |14 enter the enlargedv space or chamber 2|@ wherein further separation of solid particles from vapors takes place. The upper portion of the vessel |15 is shown as restricted on the drawing and is provided with additional separating means 228 thereon for separating additional quantities oi solid particles from the reaction products. Instead ot having the separating means 220 the upper portion of the outer vessel |18 may be enlarged to form a separating chamber or settling chamber and in this case the further separating means 228 such as cyclone separators may be eliminated. Y

The vaporous reaction products leave the top of the vessel |15 through line 22| and are preferably passed to the bottom portion oi' a fractlonating tower similar to that shown in Figure l of the drawings.

In the form of the invention shown in Figure 3 of the drawings the regenerator is shown in an elevated position and is of the bottom draw-off type whereas the reactor is of the upilow type and is arranged near the ground level. In this form i the invention the liquid feed is introduced through line 230 and is mixed with hot regenerated solid particles introduced into the mixing chamber 23| from standpipe 282 having a control valve 234. The mixture is passed through line 238 and upwardly `through a high velocity upilow reactor 288 wherein the solid particles and oii vapors are mixed and the oil is converted to lower boiling hydrocarbons. In this type of reactor the vaporous reaction products and the solid particles pass overhead from the top o the reaction zone 228. 'I'he upper portion of the reaction zone 238 is provided with a spiral separator move volatile hydrocarbons and 'the 'Uy ii troducing a suitable stripping gas such as' steam through line 258. These solid particles are also maintained in a uidized condition and dow into a standplpe 288 provided with a control valve 282 and then to a mixing chamber 282. Regenerat ing gas is introduced into the mixing chamber 288 by means of line 284 and the mixture of solid particles and gas is passed through line 288 and upwardly through line 288 into the bottom f portion of a regeneration zone 212. The iluidized tively dense condition and the pressure formed i 242 to-give the suspension a spiral inotion and to assist in separating solid particles from vaporous reaction products.

Arranged above the top of the reaction zone 238 is an enlarged chamber 264 into which the top of the reaction zone discharges. Due to the enlarged area for gas tlow, the velocity of the vapors and gases is decreased and there is a separation oi solid particles from vapors and gases.

The solid particles are collected in an annular Y chamber 248 surrounding the upper portion of the reaction zone 238 and forming part of the enlarged chamber 244 surrounding the upper portion of the reaction zone 238. The level of the separated solid particles in the annular chamber 248 is shown at 248. v

The separated reaction products in vapor form pass upwardly into the restricted portion 25| of the outer vessel 244 and preferably pass through additional separating means 252 such as dlagrammatically shown cyclone separators for separating additional quantities of solid particles from the vapors. Instead of restricting the upper portion of the vessel 244, the chamber may be enlarged to form an additional settling chamber and in this event the separating means such as cyclones shown diagrammatically at 252 may be omitted.

The separated vaporous reaction products leave the top of the enlarged chamber 244 through line 254 and are preferably passed to a ircctionating tower similar to that shown in Figure 1 of the drawings. i

The spent or fouled solid'particles in the annular space 248 are preferably stripped to refouied solid particles are maintained in al reis# by the head of iiuidized solid particles extending from the level 268 to the valve 282 is sumcientfto return the relatively light suspension passing through lines 288 and 288 to the regeneration zone 212.

In Figure 3 the chamber 244 is under about 8 pounds per square inch pressure whereas theregeneration zone 212 is under about 1 pound per square inch pressure. With these pressures and with the columns of iluidized solid particles including standpipes 282 and 258, the flow of the streams of fiuidized solid particles is as above described. i

The solid particles to be regenerated are lntroduced into the regeneration zone 212 below the perforated distribution plate 214. In the regeneration zone 212 the particles are maintained in a iiuidized condition during regeneration and the mass has a level as shown -at 218. As above pointed out in connection with Figures 1 and 2, level 218 may similarly be varied. The velocity of the regenerating gas is so selected or mainf tained that there is some settling of the particles.

and a iluidized mixture is formed. The regeneration gases leaving the fluidized mixture pass up wardly into settling space 218' and then into the restricted portion 211 of the regeneration vessel in Figure l of the drawings. Instead of having the upper portion of the vessel 212 restricted at 211 the vessel may have an enlarged dome to provide additional settling space and in this case the additional separating means 218 may be eliminated.

The regenerated solid particles are withdrawn` in fiuidized condition from a withdrawal compartment 284 shown as extending above the distribution plate 21d and communicating with the Vstandpipe 232. Preferably, a stripping gas such as steam is introduced into the withdrawal chamber 286 through line 288 to remove residual oxygen-containing gas from the hot regenerated solid particles.

To accelerate vaporiz'ing, the oil stream is preferably subdivided into a plurality of smaller streams when it is mixed with the hot solid particles from the standpipes I4 (Figure l), |84 (Figure 2) and 232 (Figure 3).

Instead of or in addition to steam or the like used to strip the hot regenerated solid particles in standpipe I4 in Figure l, hopper |82 in Figure 2 and Withdrawal chamber 286 in Figure 3, a combustible gas such as a hydrocarbon gas may be introduced through lines 88, 2|8 and 288, respectively, to reduce the oxygen concentration in the regenerated solid particles.

As above described, the invention as shown in l oi' reaction would be feed may be preheated by at a plurality of places in cracking hydrocarbons may y such as acid treated bentonite clay, synthetic -gels containing silica and alytic cracking .properly bonaceous material from. Consequently,

der to have a. sulcient quantity of solid particles to provide the necessary heat it is often necessary to substitute inert solicil material for a portion of the catalyst particles. If only catalyst were used, the catalyst to oil ratio would be high, the time extremelyshcrt and it would be impossible to control the reaction in most cases. The mixture of solid particles and catalyst particles during regeneration is heated to a temperature higher than the cracking tem.- perature and these solid particles are directly mixed with the liquid oil to raise the oil to a cracking temperature.

When of a low coke-formingstock, the oil indirect heat `exchange the process but a separate ired coil or heat' furnace for vaporizing the oil is not required. 'I'he catalyst for be any suitable one alumina `or silica and magnesio.. The' inert solid material maybe pumice, sand, kieselguhr. or any other similar material. The catalyst particles and the solid heat carrier material are preferably of such size,

to select the catalyst particles smaller or lighter than the inert particles. oi! type of reactor and regenerator described in this application there would be a tendency for the smaller and lighter particles to remain longer in the vessels than the heavy. large par- In the bottom drawticles which would be able to fall into the catalystA withdrawal spaces more readily. Thus, in catselected inert material would normally contain no carbonaceous material after passing through the cracking zone.

-shape and density that there is substantially no.

particles during the operation Consequently, it is not necessary that it ire-,

main in the regeneration zone any longer than necessary for the absorption oi' its proportionate share of the heat of regeneration. This time is much shorter than would be necessary if carif the batalyst particles are either lighter or smaller than the inert particles it is sometimes possible to decrease the total pounds of solid held in the regenerator with a resultant saving in the regenerator cost.

Conversely, if the inert particles are so selected that they aresmaller or lighter than the catalyst particles, the catalyst residence time may be decreased and in some reactions this is desirable. Where insuillcient heat is produced during regeneration in the regeneration zones or vessels shown in the drawings, further heat may be supplied to the solid particles by firing the regeneration zones. Or, if the amount of heat produced during regeneration varies due to different amounts of carbonaceous deposits onY the had to be removed there- In order to supply the heat of solid particles from diii'erent oil stocks, the heat produced in the regeneration zone may be maintained substantially constant by firing the regeneration zone. For

this firing suitable combustion material sufch as fuel oil or the like is vintroduced into the bottom portion of the re- 54 and 56. In Figure 2 the combustible material is preferably introduced into the regeneration zone 2M through line 302 and in Figure 3 through line 304 below distribution plate 274.

In Figures 2 and 3 the levels ill, 20|, 248 and 2li are similar to levels 22 and 82 described in connection with Figure 1.

In the form of the invention shown in Figure 1 of the drawings where it is desired to have about 45% conversion to gasoline of a reduced crude oil the cracking temperature is about 980 F. and the regeneration temperature is about 1150 F. vaporization and cracking, the ratio of solid material to gas oil by weight is about 18 to 1. 'I'he catalyst is included in this solid to oil ratio and the amount of catalyst is about in the proportion of about 5 parts of catalyst to 1 part oi oil by weight. The velocity of the vapors and gases in the reaction zone and regeneration zone is about 1.5 feet per second. Under theseconditions about 5.4% carbon by weight is deposited on the solid particles and after regeneration about 1% carbonaceous material by weight remains on the regenerated solid particles. Depending on the coke-forming characteristics of the stock, the oil feed may be preheated to temperatures from about` F. to 650 F. the higher temperatures giving lower carbonaceous deposits thanthe lower` temperatures.` With higher regeneration temperatures the amount of solid to oil used will be reduced. I In the reaction zone I0 the iluidized mixture has a density of about 19.5 pounds per cubic foot and the density of the suspension passing upwardly in lines 54 and 56 is about 2 pounds per cubic foot. The regenerator is Amaintained under a pressure of about 1 pound per square inch gauge and-the reaction zone is maintained undera pressure of about,8 pounds per square inch gauge. The reason for maintaining the reaction zone under a slight pressure is to provide suiilcient pressure to overcome pressure drop through the lines and through the fractionating tower 4I.

In the form of the invention shown in Figure 2 the regeneration zone 204 is supported near ground level. Substantially the same conditions and results are obtained in this form of the invention as disclosed in connection with Figure 1 except that the velocity oi?v the regenerating gas 1s about 3 feet per second.

In Figure 3 of the drawings the conditions of catalytic conversion or oils, it isl to be undersecond and the density of the been 'particularly dealso`be used in other catalytic spirit of the invention,

or hydrocarbons. hydroiormingcffhydrocarbons, A

conversions of hydrocarbons or other; catalytic reactions generally where the reactants are availabledn vaporz-or gas iormzand in'these-cases regenerated hot, solid particlesare. mixed :with

. My'invention may also be used-for carrying out Y such vapors or-gases to raise themto temperature without .using a vaporlzing furnace. While several i'orms of the invention have been shown and specific conditions and proportions given with respect to the particular forms shown,

it is to be understood that these are by way-of'l illustration only and various changes and modifications may be made without departing from the Ivclaimz. v #1..1Anpvapparatus od the character described.

y adapted, for carrying out'catalytic reactions in` cludlng'a regeneration vessel at a higher level than a reaction vessel, said reaction vessei comprising a relatively shallow cup-shaped vessel,"

means for passing hot regenerated solid particles including catalytic and inert solid particles in fiudilzed condition from said regeneration vessel into said reaction vessel, means for introducing liquid feed into said reaction vessel, an 'overow vessel for receiving fouled solid particles in tluid ized condition from said reaction vessel and hydrostatic pressure means for returning said fouled solid particles to said regeneration vessel.

2. An apparatus adapted for the treatment of solids and gases comprising an outercylindrical member having upper and lower end walls forminner compartment.

reactions nicnas oxidation,V reduction,I rcnzrrnirurins an enclosed vessel. -la cenduitieadinrlmm the uppercnd of said vessel torsvithdrawin! dal therefrom, means Amounted in the upper-'portion vof said vessel .for separatingsolids `from IISG! so withdrawn, a conduit connected to the bottom cal member and disposed in the lower partA '2o thereof,- the upper body, portion of saldcupt I shaped member having a uniformcross-section' throughout whereby the upperfendof said innery member is infree and unobstructed communica..A tion with said vessel, means for introducing-a1 Vuid stream and finely divided solids into said.

inner member and means for passing a separate stream of gas upwardly through said annular space between said inner cylindrical member and said outer cylindrical member.

3. In the apparatus defined by claim 2 in which separate means are provided for introducing said fluid stream and finely divided solids into said HOHER Z. MARTIN. 

